单击此处编辑母版标题样式,单击此处编辑母版文本样式,第二级,第三级,第四级,第五级,*,年产1万吨烯丙基氯生产流程设计,一、项目概述,氯丙稀的理化,性,性质,毒性分析,氯丙烯生产方,法,法,丙烯高温氯化,法,法,丙烯氧氯化法,氯丙烯的应用,South China University of Technology,市场调研,国外氯丙烯的,生,生产和消费情,况,况,South China University of Technology,国内环氧氯丙,烷,烷的生产和消,费,费情况,South China University of Technology,市场前景,预,预测,几年前氯,丙,丙烯主要,用,用于环氧,氯,氯丙烷的,生,生产，但,是,是随着科,技,技的发展,和,和氯丙烯,下,下游产品,的,的不断开,发,发，氯丙,烯,烯在精细,化,化工方面,的,的用途越,来,来越广，,产,产品缺口,也,也在不断,增,增大。特,别,别是去年,上,上半年一,直,直到现在,，,，氯丙烯,价,价格不断,上,上涨，处,于,于供不应,求,求状态。,随,随着国民,经,经济的快,速,速发展，,市,市场前景,将,将更加广,阔,阔，需求,会,会进一步,扩,扩大，抓,住,住机遇，,加,加快速度,完,完成1万,吨,吨规模的,氯,氯丙烯生,产,产装置的,扩,扩建。,South China University of Technology,项目设计,目,目标,（1）生,产,产方法，,原,原料及产,品,品规格,生产方法,：,：丙烯高,温,温氯化法,原料：丙,烯,烯98%，氯气,产品:,氯,氯丙烯99.9%，2-,氯,氯丙烯95%，,2,3-,二,二氯丙烯95%,，,，盐酸31.5wt%,（2）设,计,计规模与,设,设计要求,估算本项,目,目一期设,计,计氯丙烯,年,年生产能,力,力1万吨,，,，生产时,间,间为340天。要,求,求最大程,度,度实现绿,色,色化生产,，,，给出一,个,个优化的,生,生产流程,设,设计方案,，,，优化操,作,作参数，,提,提高丙烯,和,和氯气等,原,原料利用,率,率，减少,公,公用工程,消,消耗，实,现,现最大的,社,社会、环,境,境和经济,效,效益。,South China University of Technology,二、工艺,选,选择及技,术,术分析,R-601,5,6,MIXER,3,4,H-601,2,VALVE,1,E-602,7,E-603,Propylene,25C,11.7bar,Chlorine,25C,6.44bar,Fluidized,Bed Reactor,8,工艺流程,South China University of Technology,美国TBWS公司,的,的氯丙烯,分,分离装置,South China University of Technology,技术分析,反应原理,主反应：,CH2CH-CH3+Cl2,CH2=CH-CH2Cl+HCl,H1=-112kJ/mol(1),副反应：,CH2CH-CH3+Cl2,CH2=CCl-CH3+HCl,H2=-121kJ/mol(2),CH2CH-CH3+2Cl2 CH2=CCl-CH2Cl+2HCl,H3=-222kJ/mol(3),CH2CH-CH3+3Cl2 3C+6HCl,H4=-306kJ/mol(4),South China University of Technology,高温氯化,反,反应过程,控,控制条件,的,的选择,(1),反,反应温度,500,左,左右，反,应,应收率较,高,高,(2),丙,丙烯/氯,气,气摩尔比,(3),反,反应时间,(4),反,反应压力,(5),丙,丙烯、氯,气,气预热温,度,度,South China University of Technology,三、流程,模,模拟与优,化,化,从装置流,程,程图可以,得,得知，V-601,，,，T-601，T-603,的,的作用,是,是分离出,粗,粗氯丙烯,中,中的HCl 和未,反,反应的丙,烯,烯。丙烯,和,和HCl,的,的分离,主,主要是T-601,完,完成的,，,，所以本,设,设计通过,改,改变T-601,的,的操作条,件,件使其一,个,个塔能够,彻,彻底分离,出,出丙烯和HCl，,从,从而节约,设,设备投资,。,。,另外，本,设,设计作了,换,换热网络,及,及能量系,统,统初步综,合,合优化分,析,析，提高,了,了能量利,用,用效率，,降,降低了操,作,作成本,Stream NO,Temperature(),-50,-50,-50,46,-57,-56,25,10,Pressure(bar),2.09,1.50,1.50,1.50,1.40,1.50,3.00,1.40,Vapor Fraction,0.0,1.0,0.0,0.0,0.0,0.087,0.0,0.0,MolarFlowrate(kmol/h),95.61,6.92,88.69,18.38,70.31,77.23,82.0,101.0,Propylene,58.08,2.72,55.36,0.55,0.0,0.01,0.0,0.01,Allyl Chloride,15.56,0.01,15.55,15.55,0.0,0.01,0.0,0.01,2-Chloropropene,0.46,0.0,0.46,0.46,0.0,0.0,0.0,0.0,di-Chloro propene,1.81,0.0,1.81,1.81,0.0,0.0,0.0,0.0,Hydrogen,Chloride,19.70,4.19,15.51,0.01,15.55,19.69,0.0,19.11,Water,0.0,0.0,0.0,0.0,0.0,0.0,82.0,81.88,模拟结果,Stream NO,13,14,16,17,18,19,20,21,Temperature(),10,-40,59,60,10,30,106,55,Pressure(bar),1.3,1.5,2.0,1.5,1.3,1.4,1.5,1.4,Vapor Fraction,1.0,1.0,1.0,0.0,0.0,0.0,0.0,0.0,MolarFlowrate(kmol/h),58.23,0.56,17.81,17.38,58.08,0.47,1.88,15.46,Propylene,57.53,0.55,0.0,0.0,58.08,0.0,0.0,0.0,Allyl Chloride,0.0,0.0,15.54,15.52,0.0,0.02,0.08,15.44,2-Chloropropene,0.0,0.0,0.46,0.01,0.0,0.45,0.0,0.01,di-Chloro propene,0.0,0.0,0.0,1.81,1.81,0.0,1.80,0.01,Hydrogen,Chloride,0.58,0.01,0.0,0.0,0.0,0.0,0.0,0.0,Water,0.12,0.0,0.0,0.0,0.0,0.0,0.0,0.0,改进后的,分,分离流程,塔T-603的灵,敏,敏度分析,塔T-604的灵,敏,敏度分析,氯丙烯生,产,产装置换,热,热流程的,改,改进,原工艺流,程,程简图,改进后流,程,程示意图,South China University of Technology,四、,全流程经,济,济衡算,原料费用,产品及副,产,产品价值,设备投资,费,费用计算,操作费用,计,计算,全流程经,济,济衡算,South China University of Technology,五、结论,本报告主,要,要做了如,下,下的改进,与,与优化：,1）改进,了,了预分离,装,装置，将,原,原有的闪,蒸,蒸塔V-601和,精,精馏塔T-603,去,去掉，通,过,过调节塔T-601的操作,条,条件，使,得,得只用一,个,个精馏塔T-601就能达,到,到原来三,个,个塔（V-601,，,，T-601，T-603,）,）才能达,到,到的分离,效,效果，使,得,得大大降,低,低了设备,投,投资。,2）对2-氯丙烯,精,精馏塔、,氯,氯丙烯精,馏,馏塔的进,料,料板位置,进,进行了优,化,化，在一,定,定的分离,要,要求下，,找,找到了使,回,回流比最,小,小的进料,板,板位置，T-603第18,块,块理论板,进,进料，T-604,第,第23块,理,理论板进,料,料为最佳,进,进料位置,，,，降低了,公,公用工程,能,能耗。,3）本设,计,计作了换,热,热网络及,能,能量系统,初,初步综合,优,优化分析,，,，提高了,能,能量利用,效,效率，降,低,低了生产,成,成本。,4）本设,计,计作了初,步,步的经济,蘅,蘅算，年,经,经济效益,非,非常好为6248.06万,元,元。,South China University of Technology,六、建议,由于时间,有,有限，所,做,做的设计,还,还有一些,不,不足的地,方,方，现提,出,出如下一,些,些改进意,见,见：,1）本,设,设计在经,济,济蘅算时,，,，还有很,多,多实际因,素,素还没考,虑,虑进去，,也,也没有作,进,进一步的,全,全程经济,潜,潜力分析,，,，应分析,产,产量、进,料,料比、转,化,化率等对,经,经济效益,的,的影响。,2）应,引,引入环境,火,火用经济,学,学分析方,法,法，将环,境,境因素考,虑,虑进化工,优,优化过程,，,，同时由,于,于现今石,油,油,等能源和,化,化工原料,价,价格波动,很,很大，本,设,设计未做,技,技术经济,评,评价。,谢 谢,！,！,